Conversion of plastics to olefin and aromatic products

ABSTRACT

A catalyst composition useful for producing olefins and aromatic compounds from a feedstock is formed from a fluidized catalytic cracking (FCC) catalyst and a ZSM-5 zeolite catalyst, wherein the amount of ZSM-5 zeolite catalyst makes up from 10 wt. % or more by total weight of the FCC catalyst and the ZSM-5 zeolite catalyst. The catalyst composition may be used in a method of producing olefins and aromatic compounds from a feedstock by introducing a hydrocarbon feedstock and the catalyst composition within a reactor, at least a portion of the reactor being at a reactor temperature of 550° C. or higher. The feedstock and catalyst composition are introduced into the reactor at a catalyst-to-feed (C/F) ratio of from 6 or greater.

TECHNICAL FIELD

The invention relates to the conversion of plastics to olefin andaromatics through pyrolysis.

BACKGROUND

Waste plastics are mostly diverted to landfills or are incinerated, witha smaller fraction being diverted to recycling. Over the years, withincreased regulations and levies on landfills, the percentage of thepost-consumer waste being recycled or incinerated for energy recovery isgradually increasing. The 2009 statistics by Plastics Europe indicatethat approximately 24.4 million tons of waste plastics were generated inEurope. Of this, 54% was treated either through recycling (22.6%) orenergy recovery (31.3%). Plastics diverted to landfills wereapproximately 46.1%. Thus, waste plastics disposal into landfills isbecoming increasingly difficult.

Pyrolysis of waste plastics to products like naphtha, ethylene,propylene and aromatics can be classified under the category offeedstock recycling of waste plastics. With the naphtha pricesincreasing dramatically, steam crackers operating on naphtha feed are ata disadvantageous position compared to steam crackers operating oncheaper gaseous hydrocarbon feeds. If a portion of the naphtha feed tothe steam crackers is replaced by an equivalent amount of products fromplastics conversion processes, like pyrolysis, the economic situationfor the steam crackers operating on naphtha feed will improve.

In order to make an impact on the economics of very large volumes incontinuous steam cracker plant operations, it is necessary that thepyrolysis process is also continuous. No large scale plants exist todaythat directly convert waste plastics in a single step to petrochemicals.Previous attempts around the world have been focused on generation ofliquid fuels from waste plastics. These plants were small in scale ormodular in nature. Reactions carried out in such small scale plants arealso carried out for longer residence times, making them less suitablefor continuous operations on larger scales. Some earlier attempts havealso focused at generating feedstocks for steam crackers from wasteplastics. These rely on the availability of steam cracker furnaces forbeing successful, however. Furthermore, conversion of these producedsteam cracker feeds in cracker furnaces would typically result inproduction of high amounts of methane, which is undesirable.

What is therefore needed is a process for the conversion of plasticsdirectly to petrochemical products, such as olefins and aromatics, thatminimize formation of methane, and that maximizes the yield of olefinsand aromatics.

SUMMARY

A method of producing olefins and aromatic compounds from a feedstock iscarried out by introducing a hydrocarbon feedstock and a catalystcomposition within a reactor, with at least a portion of the reactorbeing at a reactor temperature of 550° C. or higher. The catalystcomposition is a fluidized catalytic cracking (FCC) catalyst and a ZSM-5zeolite catalyst, wherein the amount of ZSM-5 zeolite catalyst makes upfrom 10 wt. % or more of the total weight of the FCC catalyst and theZSM-5 zeolite catalyst. The feedstock and catalyst composition areintroduced into the reactor at a catalyst-to-feed ratio of from 6 orgreater. At least a portion of the feedstock is allowed to be convertedto at least one of olefins and aromatic compounds within the reactor. Aproduct stream is removed containing said at least one of olefins andaromatic compounds from the reactor.

In certain specific embodiments the FCC catalyst is comprised of atleast one of an X-type zeolite, a Y-type zeolite, a USY-zeolite,mordenite, faujasite, nano-crystalline zeolites, MCM mesoporousmaterials, SBA-15, a silico-alumino phosphate, a gallophosphate, and atitanophosphate.

The FCC catalyst may also comprised of at least one of a Y-zeolite and aUSY-zeolite embedded in a matrix, with the FCC catalyst having a totalsurface area of from 100 m²/g to 400 m²/g, coke deposition in an amountof from 0 to 0.5% by weight.

In some applications the FCC catalyst is a non-fresh FCC catalyst havingfrom greater than 0 to 0.5% by weight of coke deposition. In certainembodiments, the FCC catalyst may have a total surface area of from 100m²/g to 200 m²/g.

In some embodiments, the amount of ZSM-5 zeolite catalyst of thecatalyst composition makes up from 10 wt. % to 50 wt. % of the totalweight of the FCC catalyst and the ZSM-5 zeolite catalyst. In otherembodiments, the amount of ZSM-5 zeolite catalyst of the catalystcomposition makes up from 30 wt. % to 45 wt. % of the total weight ofthe FCC catalyst and the ZSM-5 zeolite catalyst.

In certain instances, the reactor may be operated wherein said at leasta portion of the reactor is at a reactor temperature of 570° C. to 730°C. The reactor may be at least one of a fluidized bed reactor, bubblingbed reactor, slurry reactor, rotating kiln reactor, and packed bedreactor in some embodiments.

In some applications, the feedstock and catalyst composition may beintroduced into the reactor at a catalyst-to-feed ratio of from 8 orgreater. The feedstock may be at least one of polyolefins, polyethylene,polypropylene, polystyrene, polyethylene terephthalate (PET), polyvinylchloride (PVC), polyamide, polypolycarbonate, polyurethane, polyester,natural and synthetic rubber, tires, filled polymers, composites,plastic alloys, plastics dissolved in a solvent, biomass, bio oils, andpetroleum oils.

In another aspect of the invention, a catalyst composition useful forproducing olefins and aromatic compounds from a hydrocarbon feedstock isprovided. The catalyst composition is comprised of a mixture offluidized catalytic cracking (FCC) catalyst and a ZSM-5 zeolitecatalyst, wherein the amount of ZSM-5 zeolite catalyst makes up from 10wt. % to 50 wt. % of the total weight of the FCC catalyst and the ZSM-5zeolite catalyst.

In certain more specific embodiments, the amount of ZSM-5 zeolitecatalyst of the catalyst composition makes up from 30 wt. % to 45 wt. %of the total weight of the FCC catalyst and the ZSM-5 zeolite catalyst.

The FCC catalyst may be comprised of at least one of a Y-zeolite and aUSY-zeolite embedded in a matrix in some applications, with the FCCcatalyst having a total surface area of from 100 m²/g to 400 m²/g, cokedeposition in an amount of from 0 to 0.5% by weight. In otherapplications, the FCC catalyst may be comprised of at least one of anX-type zeolite, a Y-type zeolite, a USY-zeolite, mordenite, faujasite,nano-crystalline zeolites, MCM mesoporous materials, SBA-15, asilico-alumino phosphate, a gallophosphate, and a titanophosphate.

The FCC catalyst may be a non-fresh FCC catalyst having from greaterthan 0 to 0.5% by weight of coke deposition. In some instances, thenon-fresh FCC catalyst may have a total surface area of from 100 to 200m²/g.

In some embodiments, the FCC catalyst may be comprised of at least oneof a Y-zeolite and a USY-zeolite embedded in a matrix, with the FCCcatalyst having a total surface area of from 100 m²/g to 400 m²/g. Incertain instances, such FCC catalyst may be a non-fresh catalyst havingfrom greater than 0 to 0.5% by weight of coke deposition. Such FCCcatalyst may further have a total surface area of from 100 m²/g to 200m²/g in some embodiments.

In certain applications, the FCC catalyst is comprised of a of at leastone of a Y-zeolite and a USY-zeolite, with said at least one of aY-zeolite and a USY-zeolite and the ZSM-5 zeolite catalyst each beingembedded in the same matrix.

BRIEF DESCRIPTION OF THE DRAWINGS

For a more complete understanding of the present invention, reference isnow made to the following descriptions taken in conjunction with theaccompanying figures, in which:

FIG. 1 is a plot of light gas olefin yields versus ZSM-5 zeolitecatalyst content of catalyst compositions used in pyrolysis conversionof a plastic feedstock;

FIG. 2 is a plot of light gas olefin yields versus reactor temperaturesin pyrolysis conversion of a plastic feedstock using a catalystcomposition of the invention;

FIG. 3 is a plot of different light gas olefin yields versus ZSM-5zeolite catalyst content of catalyst compositions used in pyrolysisconversion of a plastic feedstock;

FIG. 4 is a plot of different light gas olefin yields versus reactortemperatures in pyrolysis conversion of a plastic feedstock using acatalyst composition of the invention;

FIG. 5 is a plot of methane and ethylene yields versus ZSM-5 zeolitecatalyst content of catalyst compositions used in pyrolysis conversionof a plastic feedstock;

FIG. 6 is a plot of methane and ethylene yields versus reactortemperatures in pyrolysis conversion of a plastic feedstock using acatalyst composition of the invention;

FIG. 7 is a plot of heavy liquid product yields versus ZSM-5 zeolitecatalyst content of catalyst compositions used in pyrolysis conversionof a plastic feedstock;

FIG. 8 is a plot of heavy liquid product yields versus reactortemperatures in pyrolysis conversion of a plastic feedstock using acatalyst composition of the invention;

FIG. 9 is a plot of aromatic yields versus ZSM-5 zeolite catalystcontent of catalyst compositions used in pyrolysis conversion of aplastic feedstock;

FIG. 10 is a plot of aromatic yields versus reactor temperatures inpyrolysis conversion of a plastic feedstock using a catalyst compositionof the invention;

FIG. 11 is a plot of coke yield versus ZSM-5 zeolite catalyst content ofcatalyst compositions used in pyrolysis conversion of a plasticfeedstock; and

FIG. 12 is a plot of coke yield versus reactor temperatures in pyrolysisconversion of a plastic feedstock using a catalyst composition of theinvention.

DETAILED DESCRIPTION

In the present invention, plastics and other hydrocarbons are convertedthrough pyrolysis to monomers with high yields of light gas olefins(e.g., ethylene, propylene and butenes) and aromatics, with low yieldsof methane. The conversion can be accomplished with a low residence time(on the order of seconds) making it ideally suited for large scalecommercial operations.

The process utilizes fluid catalytic cracking (FCC) catalysts and aZSM-5 zeolite catalyst additive that are used in combination with oneanother in a catalyst composition to facilitate the pyrolytic conversionof the plastic or hydrocarbon feed. The FCC catalysts are those usefulin the cracking of petroleum feeds. Such petroleum feeds may includevacuum gas oil (350-550° C. boiling range), atmospheric gas oil anddiesel (220-370° C. boiling range), naphtha (<35° C. to 220° C. boilingrange) or residues (boiling at >550° C. range) from a crude oilatmospheric and vacuum distillation units or the various such streamsgenerated from all secondary processes in refineries includinghydrotreating, hydrocracking, coking, visbreaking, solvent deasphalting,fluid catalytic cracking, naphtha reforming and such or their variants.The FCC catalysts are typically composed of large pore molecular sievesor zeolites. Large pore zeolites are those having an average pore sizeof from 7 Å or more, more typically from 7 Å to about 10 Å. Suitablelarge pore zeolites for FCC catalysts may include X-type and Y-typezeolites, mordenite and faujasite, nano-crystalline Zeolites, MCMmesoporous materials (MCM-41, MCM-48, MCM-50 and other mesoporousmaterials), SBA-15 and silico-alumino phosphates, gallophosphates,titanophosphates. Particularly useful are Y-type zeolites.

In Y-type zeolites used for FCC catalysts, the silica and aluminatetrahedral are connected by oxygen linkages. In order to impart thermaland hydrothermal stability, the Y-zeolite may be subjected to treatmentto knock off some framework alumina (one of these routes is steaming athigh temperature). Typically Y-zeolites have Si/Al ratio of about 2.5:1.The dealuminated Y-zeolite typically has a Si/Al ratio of 4:1 or more.The dealuminated Y-zeolite, with a higher framework Si/Al ratio, hasstronger acid sites (isolated acid sites) and is thermally andhydrothermally more stable and is thus called ultrastable Y-zeolite(USY-zeolite). In units like fluid catalytic cracking where thecatalysts see temperatures of 700° C. and also moisture in a catalystregenerator, the thermal and hydrothermal stability is important so thatcatalyst activity is maintained over a longer period of time. Hence, insuch types of operation USY-zeolite may be the preferred FCC catalyst.

The ultrastable zeolites may also be rare-earth-exchanged. Therare-earth content may be higher than 0% and may be as high as 10% byweight of the zeolite, with from 0.1-3% by weight of zeolite beingtypical. The higher the rare earth content, however, the moreolefinicity of the products is lost by favoring hydrogen transferreactions to make paraffins. Some amount of rare earth in the zeolite Ymay be useful because it imparts stability to the zeolite. The rareearth materials may include cerium, lanthanum and other rare earthmaterials.

It should be understood that with respect to any concentration or amountrange listed or described in the summary and detailed description asbeing useful, suitable, or the like, it is intended to include everyconcentration or amount within the range, including the end points, andis to be considered as having been specifically stated. For example, “arange of from 1 to 10” is to be read as indicating each and everypossible number along the continuum between about 1 and about 10. Thus,even if specific data points within the range, or even no data pointswithin the range, are explicitly identified or refer to only a specificfew, it is to be understood that the inventors appreciate and understandthat any and all data points within the range are to be considered tohave been specified, and that the inventors are in possession of theentire range and all points within the range.

The FCC catalysts are typically the afore-mentioned zeolites embedded inan active matrix. The matrix may be formed from an active material, suchas an active alumina material that could be amorphous or crystalline, abinder material, such as alumina or silica, and an inert filler, such askaolin. The zeolite component embedded in the matrix of the FCC catalystmay make up from 10 to 90% by weight of the FCC catalyst. The FCCcatalyst with the zeolite material embedded within the active matrixmaterial may be formed by spray drying into microspheres. Thesecatalysts are hard and have very good attrition resistance to withstandthe particle-particle and particle-wall collisions that usually occurwhen the catalysts are fluidized. The particle size distribution for theFCC catalyst may range from greater than 0 to 150 microns. In certainembodiments, 90-95% of the particle size distribution may be within therange of from greater than 0 to 110 microns or 120 microns, with from5-10% of the particles having particle sizes of greater than 110microns. As a result of the distribution of particle sizes, the averageor median particle size for the FCC catalyst is typically 70 to 75microns. In certain instances, finer particles of the FCC catalyst maybe used with larger particles to provide good fluidization. In certainembodiments, for example, 15% or less of the FCC catalyst may have aparticle size of 40 microns or less. Good fluidization is imparted bypresence of fines in a mix of fine and coarse particles. Loss of fineparticles leads to de-fluidization.

The FCC catalysts may be further characterized based on certainphysical, chemical, surface properties and catalytic activity. Fresh FCCcatalysts have a very high surface area typically 300-400 m²/g or higherand a high activity. As a result of the high activity of the fresh FCCcatalyst, cracking of petroleum feeds with the fresh FCC catalystusually results in high yields of coke, such as 8-10 wt. %, and lightgas. The very high yields of coke can affect the heat balance of thereaction as all the heat generated by coke formation may not be neededfor cracking. Heat removal from a reactor-regenerator system thus may benecessary. This means that the feed is not effectively utilized. Itwould be more economically valuable if just enough coke required forsupporting the cracking process heat requirements was made, with thebalance that otherwise goes into excess coke formation being used toform useful products. Also, high yields of light gases (methane, ethane)from the fresh FCC catalyst are undesirable and may exceed the plant wetgas compressor equipment constraints or limits in an FCC complex. Highyields of methane are undesirable because of its limited utility informing chemicals (even though it is possible to form higherhydrocarbons from methane through syngas-methanol-olefins route). Ethaneon the other hand may be used for making ethylene, a valuable chemical.In most cases, however, higher ethane yield is accompanied by a highermethane yield.

In order to overcome these problems, the FCC cracking unit is typicallyoperated by maintaining a constant activity or conversion. This is doneby having a circulating inventory of partially deactivated catalyst andthen periodically purging a small portion of the used or non-freshcatalyst and making that up with fresh FCC catalyst. The use of used ornon-fresh catalyst helps in maintaining the catalyst activity at aconstant level without producing high levels of methane and coke. Thecirculating inventory of plant catalyst is partially deactivated orequilibrated under plant operating conditions. The portion of thiscatalyst that is purged out periodically is the spent catalyst. Thus interms of catalyst activity it generally has the same activity of thecirculating catalyst inventory in the FCC unit before make-up freshcatalyst is added. This catalyst make-up and purging is typically doneon a regular basis in an operating FCC unit. The circulating catalystinventory has roughly 50% or less of the surface area of the freshcatalyst and activity or conversion that is roughly 10 conversion unitslower than that of fresh catalyst. In other words, if fresh catalystwere to provide a conversion of 80 wt. % of vacuum gas oil rangematerial to dry gas (H₂—C₂), LPG (C₃-C₄), gasoline (35-220° C. boilinghydrocarbons) and coke, then the circulating partially deactivatedcatalyst inventory could provide a conversion of 70 wt. %. The FCC freshcatalyst particles added through make-up to the circulating unit wouldon an average spend several days (age) in the unit before it is purgedout. Thus, due to the fact that daily make-up is made to the catalystinventory, the circulating catalyst inventory would typically havecatalyst particles of different ages, i.e., there is an age distributionof catalyst particles in the inventory. The catalyst activity of aparticle is proportional to its deactivation in the FCC unit which inturn is also proportional to the age of the catalyst. The followingTable 1 below lists typical properties between fresh and spent FCCcatalysts.

TABLE 1 Fresh FCC Property Catalyst Spent FCC Catalyst Total surfacearea, m²/g 320-360 130-170 Unit cell size, angstroms 24.4-24.7 24.2-24.4Conversion of standard 78-85 67-73 petroleum feed or activity, wt % Ni +V, ppm 0 Typically 500-3000 Coke on the catalyst, wt % 0 0-0.5 typicallySulfur oxide (Sox) reduction No Yes* and/or Sulfur reduction additivespresent? *Sox and S reduction additives are usually from 10-15 wt. %.Sox and S reduction additives would not have catalyst activity forcracking and thus would dilute the catalyst activity. These additivesare usually added to meet automotive fuel specification requirements forstreams generated from the FCC unit and for mitigating Sox liberation toenvironment. Usually oxides of magnesium are used in such additives andthey would be having lower or no conversion for breaking molecules andwould thus reduce the ability of the FCC catalyst to convert heaviermolecules to lighter molecules i.e. activity dilution.

The present invention can make use of either fresh FCC catalyst,non-fresh FCC catalyst, or a mixture of both. This may include spent FCCcatalyst that is removed from the fluidized catalytic cracking process,as described previously. Because spent FCC catalyst is typically a wasteproduct from the fluidized catalytic cracking process, its use in theconversion of plastics and other hydrocarbons to useful products isparticularly advantageous. This is due to both its lower cost andavailability and due to its favorable activity in not forming more cokeand methane. The spent FCC catalyst is essentially “used” or “non-fresh”FCC catalyst that has been used in the fluidized catalytic crackingprocess and has been removed for replacement with fresh catalyst, aspreviously described. As used herein, the expression “non-fresh” withrespect to the FCC catalyst is meant to encompass any FCC catalyst, asthey have been described, that has some amount (i.e. greater than 0%) ofcoke deposition. Fresh FCC catalyst would have no coke deposits. In someembodiments, the coke deposition on the non-fresh FCC catalyst may befrom 0.01%, 0.05%, 0.1%, 0.2%, 0.3%, 0.4% or more by weight of thecatalyst. Typically, the coke deposition for the non-fresh FCC catalystwill range from greater than 0 to 0.5% by weight of the catalyst. Thespent FCC catalyst may have non-fresh catalyst particles with differingdegrees of catalyst coking due to differences in the catalyst ages ofuse in the cracking process. The non-fresh FCC catalyst also has areduced surface area compared to fresh FCC catalyst due to catalysthydrothermal deactivation in the FCC unit. Typical surface area for thenon-fresh catalyst may range from 100 m²/g to 200 m²/g. Additionally, insome embodiments the FCC catalyst may include a combination of non-freshor spent FCC catalyst and fresh FCC catalyst and may be used in thepyrolysis conversion reaction.

The ZSM-5 zeolite catalyst additive used in combination with the FCCcatalyst is a molecular sieve that is a porous material containingintersecting two-dimensional pore structure with 10-membered oxygenrings. Zeolite materials with such 10-membered oxygen ring porestructures are often classified as medium-pore zeolites. Suchmedium-pore zeolites typically have pore diameters ranging from 5.0 Å to7.0 Å. The ZSM-5 zeolite is a medium pore-size zeolite with a porediameter of from about 5.1 to about 5.6 Å. The ZSM-5 zeolite and theirpreparation are described in U.S. Pat. No. 3,702,886, which is hereinincorporated by reference. The ZSM-5 zeolite may be free from any metalloading.

The ZSM-5 zeolite is also typically embedded in an active matrix, whichmay be the same or similar to those used for the zeolite of the FCCcatalyst, as previously described. The matrix may be formed from anactive material, such as an active alumina material, a binder material,such as alumina or silica, and an inert filler, such as kaolin.

The zeolite component embedded in the matrix of the ZSM-5 catalyst maymake up from 5 to 90% by weight of the ZSM-5 zeolite catalyst and moretypically between 10 to 80% by weight of the ZSM-5 zeolite catalyst, andstill more typically between 10 to 50% by weight of the ZSM-5 zeolitecatalyst. The ZSM-5 zeolite catalyst with the ZSM-5 zeolite materialembedded within the active matrix material may also be formed by spraydrying into microspheres. The particle size distribution for the ZSM-5zeolite catalyst may range from greater than 0 to 150 microns. Incertain embodiments, 90-95% of the particle size distribution may bewithin the range of from greater than 0 to 110 microns or 120 microns.The average or median particle size for the ZSM-5 zeolite catalyst istypically 70 to 75 microns. In certain instances, finer particles of theZSM-5 zeolite catalyst may be used with larger particles to provide goodfluidization. In certain embodiments, for example, 15% or less of theZSM-5 zeolite catalyst may have a particle size of 40 microns or less.

In certain embodiments, the zeolite material (e.g. X-type zeolite orY-type zeolite) of the FCC catalyst and the ZSM-5 zeolite may beembedded and formed within the same matrix material unit so thatcatalyst particles containing both the FCC catalyst and ZSM-5 catalystmaterials are formed. These particles may be of the same size andconfiguration as those previously described for the separate FCCcatalyst and ZSM-5 zeolite catalyst. One of the advantages of combiningthe FCC and ZSM-5 zeolite component in a single matrix or particle isthat it may result in a higher activity that can be obtained byminimizing the in-active diluents in the individual catalysts.

The catalysts selected for use in the plastic pyrolysis may have similarproperties to FCC catalysts in terms of particle size distribution andattrition resistance, as these parameters may greatly influence theintegrity of the catalyst recipe in an operating fluidized bedenvironment. Very fine particles can lead to their high losses due totheir being entrained with product gases, while bigger catalyst particlesizes tend to not fluidize properly and result in non-uniform activity.In certain embodiments, however, pure forms of the FCC catalyst and theZSM-5 zeolite without any matrix material or smaller particle sizes maybe employed in systems where there is less probability of the catalystbeing lost, such as in rotary kilns and slurry reactors.

In the present invention, plastic pyrolysis using the catalyst systemproduces valuable monomers of light gas olefins and aromatics, such asbenzene, toluene and xylenes. The process yields are tunable to thedesired yields of olefins and aromatics by using a combination of thecatalyst system and process operating conditions. It has been found thatwith a combination of FCC catalysts and ZSM-5 zeolite catalyst additive,as has been described, higher yields of olefins and aromatics can beobtained as compared to using only an FCC catalyst. Specifically, acatalyst system containing from 10 wt. % or more of ZSM-5 zeolitecatalyst of the total weight of the FCC catalyst and the ZSM-5 zeolitecatalyst provides increased yields of olefins and aromatics. As usedherein, weight percentages of the ZSM-5 zeolite catalysts and FCCcatalysts are based upon the total weight of the catalyst, including anymatrix material, unless expressly stated otherwise. Where no matrixmaterial is employed in the reactions the weight percentages of theZSM-5 zeolite catalysts and FCC catalysts are the weight percentage ofthe zeolites only.

In certain embodiments, the amount of ZSM-5 zeolite catalyst of thecatalyst composition makes up from 10 wt. % to 50 wt. % of the totalweight of the FCC catalyst and the ZSM-5 zeolite catalyst. Thus, theamount of ZSM-5 zeolite catalyst of the catalyst composition makes upfrom 10 wt. %, 15% wt. %, 20% wt. %, 25% wt. %, 30% wt. %, or 35% wt. %to 40% wt. %, 45% wt. %, or 50 wt. % of the total weight of the FCCcatalyst and the ZSM-5 zeolite catalyst. In still other embodiments, theamount of ZSM-5 zeolite catalyst of the catalyst composition makes upfrom 30 wt. % to 45 wt. % of the total weight of the FCC catalyst andthe ZSM-5 zeolite catalyst. In further embodiments, the amount of ZSM-5zeolite catalyst of the catalyst composition makes up from 35 wt. % to40 wt. % of the total weight of the FCC catalyst and the ZSM-5 zeolitecatalyst. In particular instances, it has been found that the highestyields of olefins and aromatics are produced when the ZSM-5 zeolitecatalyst is used in an amount of approximately 37.5 wt. % by totalweight of the FCC catalyst and the ZSM-5 zeolite catalyst.

The plastic feed used in the conversion reaction may include essentiallyall plastic materials, such as those formed from organic polymers.Non-limiting examples include polyolefins, such as polyethylene,polypropylene, etc., polystyrene, polyethylene terephthalate (PET),polyvinyl chloride (PVC), polyamide, polycarbonate, polyurethane,polyester, natural and synthetic rubber, tires, filled polymers,composites and plastic alloys, plastics dissolved in a solvent, etc.While plastic feeds may be used in the conversion reaction, otherhydrocarbon materials may also be used as the feedstock. Thesehydrocarbons may include biomass, bio oils, petroleum oils, etc. Thus,while the present description is directed primarily to the conversion ofplastic feeds, it should be understood that the invention hasapplicability to and encompasses the use of other hydrocarbons as well.When production of light gas olefins is desired, a plastic feed ofpolyolefins or that is primarily or contains a substantial portion ofpolyolefins may be preferred. Mixtures of various different plastic andhydrocarbon materials may be used without limitation.

The plastic feed may be provided in a variety of different forms. Insmaller scale operations, the plastic feed may be in the form of apowder. In larger scale operations, the plastic feed may be in the formof pellets, such as those with a particle size of from 1 to 5 mm.

The catalyst and plastic feed may be mixed together prior tointroduction into the reactor or may be fed separately. The amount orratio of catalyst used to plastic feed may vary and may be dependentupon the particular system used and process conditions. Plastics can beconverted using a very low or very high catalyst-to-feed (C/F) ratio.Longer contact times may be needed in the case of a low C/F ratio, whileshorter contact times may be need for a high C/F ratio. In testing, C/Fratios of from 4 to 12 were used, with C/F ratios of from 6 to 9 beingmost frequently used. In large scale industrial process wherein acirculating fluidized bed riser or downer may be used, the C/F ratio maybe determined by the reactor heat balance or other parameters.

Various reactors may be used for the conversion process. For large scaleoperations, a circulating fluidized bed riser or downer reactor may beused. A bubbling bed reactor where the catalyst is bubbled in-situ, withthe feed being added to the bubbling bed may also be used. Slurry-typereactors and rotating kiln-type reactors may also be used in someapplications.

The catalyst composition composed of the FCC catalyst and ZSM-5 zeolitecatalyst and the plastic feed are introduced (mixed or added separately)into a reactor, such as a fluidized bed reactor, as previouslydescribed. The reactor is operated at a reactor temperature wherein allor a portion of the reactor is at a temperature of 550° C. or higher. Insome embodiments, the reactor is operated at a reactor temperaturewherein all or a portion of the reactor is at a temperature of 570° C.or higher. In certain embodiments, the reactor is operated at a reactortemperature wherein all or a portion of the reactor is at a temperatureof from 550° C. to 730° C., more particularly from 570° C. to 680° C.,690° C. or 700° C. Reactor pressures may range from ambient to 50 bar(g) (5 MPa) and more typically from ambient to 3 bar (g) (0.3 MPa).Nitrogen, dry gas (H₂—C₂), steam or other inert gases or mixture ofgases may be used as a carrier gas in which the catalyst and feed areentrained. A range of fluidization gas flow rates can be employed indifferent modes, such as bubbling fluidized bed mode, circulatingfluidized bed mode, slurry tank reactor mode. Other reactorconfigurations and modes may also be used. In particular embodiments, acirculating fluidized mode may be used because it offers advantages oncoke management, better heat transfer and contacting between feed andcatalysts. The catalyst/feed ratio (C/F) can range from as low as 2 andas high as 30 and more typically in the range of 4-12.

The pyrolysis conversion of plastics to light gas olefins and aromaticsmay take place fairly rapidly, i.e. within a few seconds. The pyrolysisproducts produced include light gas olefins, such as ethylene,propylene, butenes, etc., and aromatics, such as benzene, toluene,xylenes, and ethyl benzene. These may be selectively produced in largequantities. Complete conversion of the feed plastics to various productsoccurs. Products produced include gases (H₂—C₄), gasoline or naphtha(boiling point 35-220° C.), diesel (boiling point 220-370° C.), a smallfraction of heavier stream (boiling point >370° C.) and coke. The yieldof various products could be varied by using different catalyst recipeor any or all of the above mentioned parameters including contact time,fluidization flow rate and specific features of the reactor hardware,such as diameter, length or feed and/or gas distribution design ormixing/contacting related hardware modifications, recycles of productsinto the reactor for further conversion and such other parameters.Saturated products, such as methane, ethane, propane, and butanes, arealso produced, as well as hydrogen gas (H₂). In testing, low yields ofmethane and butadiene were obtained (<2 wt. % and 0.5 wt. %,respectively). This indicates that even though the temperature severityemployed is high (i.e. 550° C. or higher), the observed activity ispredominantly probably due to catalytic activity than thermal cracking.The catalyst composition can be used under conditions that successfullysuppress methane formation and at the same time offer high conversionsand minimize heavy products. The process also minimizes the formation ofheavy liquid products, i.e., those product heavy ends boiling above 370°C.

The pyrolysis products produced can be used in a variety of processes.For example the light gas olefins formed (ethylene, propylene andbutenes) can be used in polymerization, the aromatics can be used asbuilding blocks for derivatives or can be used as such in specificapplications, the saturated gases can be cracked further to light gasolefins or can be directed to fuel gas (H₂—C₂) and LPG (C₃-C₄) pool orcan be used as a fuel in the pyrolysis or any other process. The cokeformed can be used as an energy source for supplying the necessary heatrequirements for the pyrolysis process.

The following examples serve to further illustrate the invention.

EXAMPLES Experimental

In each of the examples presented below, an in-situ fluidized bed labtubular reactor having a length of 783 mm and an inner diameter of 15 mmwas used. The reactor was housed in a split-zone 3-zone tubular furnacewith independent temperature control for each zone. The size of eachzone was 9.3 inches (236.2 mm). The overall heated length of the reactorplaced inside the furnace was 591 mm. The reactor wall temperature wasmeasured at the centre of each zone and was used to control the heatingof each furnace zone. The reactor had a conical bottom and the reactorbed temperature was measured using a thermocouple housed inside athermowell and placed inside the reactor at the top of the conicalbottom. Also, the reactor wall temperature was measured at the conicalbottom to ensure that the bottom of the reactor was hot. The reactorbottom was placed at the middle of the furnace bottom zone forminimizing the effect of furnace end cap heat losses and maintaining thereactor bottom wall temperature within a difference of 20° C. of theinternal bed temperature measured.

The plastic feeds were in the form of a 200 micron plastic powder. TheFCC catalyst was a spent FCC catalyst obtained from an operatingrefinery. The FCC spent catalyst used had a residual coke on it of 0.23wt %. The ZSM-5 zeolite catalyst used was a commercially available ZSM-5zeolite catalyst. The plastic feed was mixed with catalyst by swirlingin a cup and then fed into the reactor.

The conversion products from the reactor were collected and condensed ina condenser. The uncondensed products were collected in a gas collectionvessel and the gas composition was analyzed using a refinery gasanalyzer (M/s AC Analyticals B.V., The Netherlands). Liquid productswere characterized for their boiling point distribution using asimulated distillation GC (M/s AC Analyticals B.V., The Netherlands). Inaddition a detailed hydrocarbon analysis (up to C₁₋₃ hydrocarbons) wascarried out using a DHA analyzer (M/s AC Analyticals B.V., TheNetherlands). The coke deposited on the catalyst was determined using anIR-based CO and CO₂ analyzer. The mass balances were determined bysumming the yields of gas, liquid and coke. Individual product yieldswere determined and reported on a normalized product basis.

Example 1

Tests were conducted using a pure HDPE plastic feed ground to 200microns size and a catalyst composition of 75 wt. % FCC spent catalystand 25 wt. % of ZSM5 zeolite catalyst. The plastic feed used was 0.75 gand the dry catalyst weight used was 4.5 g. This correlates to a C/Fratio of 5.98 (˜6.0). The feed and the catalyst were fed to the reactoras described above. Before charging of the feed, the bed temperature asmeasured by the reactor internal thermocouple was 650° C. A flow of N₂gas at 200 Ncc/min (normal cc/min) was used as a fluidizing and carriergas. The results are presented in Table 2 below.

TABLE 2 C/F ratio 6.0 Reaction temperature at start 650.0 Methane 1.24 %H2, C1, C4 yield 54.1 % Liquid yield 44.2 % Coke yield 1.7 C4=, wt %16.3 C3=, wt % 19.8 C2=, wt % 6.3 Total olefins 42.4This example shows that with pure polyolefinic feed, high gas yield ispossible at high temperature severity without producing high yields ofmethane.

Experimental for Examples 2-13

For Examples 2-13, a mixed plastic feed formed from a mixture ofpolyolefins, polystyrene (PS) and PET was used having the followingcomposition set forth in Table 3 below. The mixed plastic was used inthe form of powder and was fed to the reactor along with catalyst asdescribed earlier. Reactor temperatures at the start of reaction arethose measured inside the reactor before feed and catalyst are charged.Fluidization N₂ gas flow was 175 Ncc/min.

TABLE 3 Material Amount HDPE 19 wt. % LDPE 21 wt. % PP 24 wt. % C4-LLDPE12 wt. % C6-LLDPE  6 wt. % PS 11 wt. % PET  7 wt. %

Example 2

Spent FCC catalyst was used with varying amounts of ZSM-5 zeolitecatalyst from 0 to 100 percent. The testing was conducted at a reactortemperature of 670° C. set before the start of reaction. A C/F ratio of9 was used. The experiments were carried out with 6.8 g of dry catalystand 0.75 g of plastic feed. The total light gas olefins (i.e., C₂ to C₄)were measured. The results are presented in FIG. 1 and Table 4. As canbe seen from FIG. 1, the highest yields of light gas olefins wasachieved when the amount of ZSM-5 zeolite catalyst additive in thecatalyst mixture was at around 37.5 wt. %.

TABLE 4 ZSM-5 zeolite catalyst Wt. % 0 25 37.5 50 100 content incatalyst mixture C/F ratio g/g 9.1 9 9 9 8.9 Reaction temperature atstart ° C. 670 670 670 670 670 Dry catalyst fed g 6.8 6.77 6.76 6.75 6.7Feed weight transferred g 0.75 0.75 0.75 0.75 0.75 Total light gasolefins Wt. % 24.5 33.4 36.4 34.2 31.5 (C₂ + C₃ + C₄) yield

Example 3

Tests to determine the effect of different reactor temperatures at thestart of the reaction and different C/F ratios of 6 and 9 on theproduction of light gas olefin yields were conducted. These experimentswere carried out by employing a catalyst mixture containing 62.5 wt. %of spent FCC catalyst and 37.5 wt. % of ZSM-5 zeolite catalyst at a C/Fratio of 9 and 75 wt. % of spent FCC catalyst and 25 wt. % of ZSM-5zeolite catalyst at a C/F ratio of 6. When the feed and catalyst wascharged, the reactor temperature fell rapidly and reached a minimumvalue and then climbed back to its original values before the start ofreaction. Most of the temperature regain occurred within one minuteafter charging of reactor. The results are presented in FIG. 2 andTables 5 and 6. As can be seen from FIG. 2, the light gas olefin yieldsincreased with temperature and reached a maximum value at or around 670°C. With a higher C/F ratio of 9 (Table 5), the olefin yield increasedcompared to the lower C/F ratio (Table 6).

TABLE 5 Catalyst Wt. % Spent Spent Spent Spent composition FCC FCC FCCFCC (62.5%) + (62.5%) + (62.5%) + (62.5%) + ZSM-5 ZSM-5 ZSM-5 ZSM-5zeolite zeolite zeolite zeolite catalyst catalyst catalyst catalyst(37.5%) (37.5%) (37.5%) (37.5%) C/F ratio g/g 9.0 7.0 9.0 9.95 Reaction° C. 600 623 670 700 temperature at start Dry catalyst g 6.76 5.22 6.767.46 fed Feed weight g 0.75 0.75 0.75 0.75 transferred Total light gasWt. % 28.58 31.32 36.35 34.16 olefins yield (C₂ + C₃ + C₄)

TABLE 6 Catalyst Wt. % Spent Spent Spent Spent composition FCC FCC FCCFCC (75%) + (77.3%) + (75%) + (75%) ZSM-5 ZSM-5 ZSM-5 ZSM-5 zeolitezeolite zeolite zeolite catalyst catalyst catalyst catalyst (25%)(22.7%) (25%) (25%) C/F ratio g/g 6.0 6.0 6.0 6.0 Reaction ° C. 600 630670 700 temperature at start Dry catalyst fed g 4.49 2.99 4.49 2.99 Feedweight g 0.75 0.5 0.75 0.5 transferred Total light gas Wt. % 28.73 30.3631.73 30.96 olefins yield (C₂ + C₃ + C₄)

Example 4

Tests to determine the yields of different olefins as a function ofcatalyst composition of spent FCC catalyst with varying amounts of ZSM-5zeolite catalyst (i.e., 0 to 100%) were conducted. The reaction wascarried out at a temperature of 670° C. at the start of reaction and aC/F ratio of 9. The results are presented in FIG. 3 and Table 7. As canbe seen in FIG. 3, propylene yields were highest at a ZSM-5 zeolitecatalyst content of about 37.5 wt. %.

TABLE 7 ZSM-5 zeolite Wt. % 0 25 37.5 50 100 catalyst content in thecatalyst mixture C/F ratio g/g 9.07 9.0 9.0 9.0 8.92 Reaction ° C. 670670 670 670 670 temperature at start Dry catalyst fed g 6.80 6.77 6.766.75 6.70 Feed weight g 0.75 0.75 0.75 0.75 0.75 transferred C₄ Yield =Wt. % 11.99 13.32 13.21 12.69 10.58 C₃ Yield = Wt. % 10.57 14.96 16.6215.28 14.21 C₂ Yield = Wt. % 1.98 5.11 6.52 6.22 6.71 Total light gas Wt% 24.5 33.4 36.4 34.2 31.5 olefins yield

Example 5

Tests to determine the effect of starting temperatures of the yields ofdifferent olefins were conducted. The amount of ZSM-5 zeolite catalystwas at 37.5 wt. % of the catalyst mixture. The C/F ratios used areprovided in Table 8. The results are presented in FIG. 4 and Table 8. Ascan be seen in FIG. 4, the highest yields were obtained at a temperatureof around 670° C.

TABLE 8 Catalyst Wt. % Spent Spent Spent Spent composition FCC FCC FCCFCC (62.5%) + (62.5%) + (62.5%) + (62.5%) + ZSM-5 ZSM-5 ZSM-5 ZSM-5zeolite zeolite zeolite zeolite catalyst catalyst catalyst catalyst(37.5%) (37.5%) (37.5%) (37.5%) C/F ratio g/g 9.0 7.0 9.0 9.95 Reaction° C. 600 623 670 700 temperature at start Dry catalyst g 6.76 5.22 6.767.46 fed Feed weight g 0.75 0.75 0.75 0.75 transferred C₄ Yield = Wt. %11.77 12.54 13.21 11.89 C₃ Yield = Wt. % 12.59 13.90 16.62 15.61 C₂Yield = Wt. % 4.22 4.89 6.52 6.66

Example 6

Tests were conducted at an initial reaction temperature of 670° C. withvarying amounts of ZSM-5 zeolite catalyst from 0% to 100% in thecatalyst composition. A C/F ratio of 9 was used. Ethylene and methaneyields were then measured, with the results being presented in FIG. 5and Table 9. As can be seen in FIG. 5 and from Table 9, methane yieldsdid not vary significantly over the range of ZSM-5 zeolite catalystcontent for the catalyst system. In comparison, the ethylene yieldsincreased significantly from 2 wt. % to 7 wt. %, indicating that methaneyields are being suppressed under the operating conditions and thecatalyst composition employed.

TABLE 9 ZSM-5 zeolite catalyst content Wt. % 0 25 37.5 50 100 in thecatalyst mixture C/F ratio g/g 9.07 9.0 9.0 9.0 8.92 Reactiontemperature at start ° C. 670 670 670 670 670 Dry catalyst fed g 6.806.77 6.76 6.75 6.70 Feed weight transferred g 0.75 0.75 0.75 0.75 0.75Methane Wt. % 1.00 0.81 0.90 0.79 1.13 Ethylene Wt. % 1.98 5.11 6.526.22 6.71

Example 7

Tests to determine the effect of starting temperatures on the yields ofmethane and ethylene were conducted. The catalyst composition was 62.5%wt. % FCC catalyst and 37.5 wt. % ZSM-5 zeolite catalyst, using a C/Ffeed ratio of 9. The results are presented in FIG. 6 and Table 10. Ascan be seen in FIG. 6, over the range of temperatures, the methaneyields varied from 0.4 wt. % to 1.3 wt. %, while ethylene yields variedfrom 4.2 wt. % to 6.7 wt. %. Again, the yields of methane were low,showing that the combination of catalyst composition and processconditions can suppress methane yields and increase ethylene production.

TABLE 10 Catalyst Wt. % Spent Spent Spent Spent composition FCC FCC FCCFCC (62.5%) + (62.5%) + (62.5%) + (62.5%) + ZSM-5 ZSM-5 ZSM-5 ZSM-5zeolite zeolite zeolite zeolite catalyst catalyst catalyst catalyst(37.5%) (37.5%) (37.5%) (37.5%) C/F ratio g/g 9.0 7.0 9.0 9.95 Reaction° C. 600 623 670 700 temperature at start Dry catalyst g 6.76 5.22 6.767.46 fed Feed weight g 0.75 0.75 0.75 0.75 transferred Methane Wt. %0.38 0.62 0.90 1.29 Ethylene Wt. % 4.22 4.89 6.52 6.66

Example 8

Tests to determine the yields of heavy liquid product (i.e., liquidproduct with a boiling point above 370° C.) as a function of catalystcomposition of spent FCC catalyst with varying amounts of ZSM-5 zeolitecatalyst (i.e., 0 to 100%) were conducted. The reaction was carried outat a temperature of 670° C. and a C/F ratio of 9. The results arepresented in FIG. 7 and Table 11. As can be seen in FIG. 7, above aZSM-5 zeolite catalyst content of 50 wt. % the catalyst activity forproducing heavy liquid products is not optimal. The catalyst activitygets diluted with higher amounts of ZSM-5 zeolite catalyst above thisrange.

TABLE 11 ZSM-5 zeolite catalyst Wt. % 0 25 37.5 50 100 content in thecatalyst mixture C/F ratio g/g 9.07 9.0 9.0 9.0 8.92 Reactiontemperature at ° C. 670 670 670 670 670 start Dry catalyst fed g 6.806.77 6.76 6.75 6.70 Feed weight transferred g 0.75 0.75 0.75 0.75 0.75Heavies Wt. % 0.64 0.50 0.39 1.54 1.48

Example 9

Tests to determine the effect of starting temperatures on the yields ofheavy liquid products (i.e., liquid product with a boiling point above370° C.) were conducted. The catalyst composition was approximately 75%wt. % FCC catalyst and 25 wt. % ZSM-5 zeolite catalyst, using a C/F feedratio of 6. The results are presented in FIG. 8 and Table 12. As shownin FIG. 8, at an initial reaction temperature of around 670° C. theheavy liquid product is very low, with increasing heavy liquid productsbeing produced as the temperature is increased.

TABLE 12 Catalyst Wt. % Spent Spent Spent Spent composition FCC FCC FCCFCC (75%) + (77.3%) + (75%) + (75%) + ZSM-5 ZSM-5 zeolite ZSM-5 ZSM-5zeolite catalyst zeolite zeolite catalyst (22.7%) catalyst catalyst(25%) (25%) (25%) C/F ratio g/g 6.0 6.0 6.0 6.0 Reaction ° C. 600 630670 700 temperature at start Dry catalyst fed g 4.49 2.99 4.49 2.99 Feedweight g 0.75 0.5 0.75 0.5 transferred Heavies Wt. % 0.22 0.11 0.11 0.66

Example 10

Tests to determine the yields of aromatics as a function of catalystcomposition of spent FCC catalyst with varying amounts of ZSM-5 zeolitecatalyst (i.e., 0% to 100%) were conducted. Aromatic product content wasdetermined in the liquid product boiling at a temperature below 240° C.The reaction was carried out at a temperature of 670° C. and a C/F ratioof 6. The results are presented in FIG. 9 and Table 13. As shown in FIG.9, the liquid product is rich in aromatic content, with even higheraromatic content in liquid product being achieved with a ZSM-5 zeolitecatalyst content of around 25 wt. % or higher.

TABLE 13 Aromatic Dry Feed content Temperature catalyst weight inliquid, Catalyst composition ° C. fed transferred Wt. % 100 wt. % SpentFCC 670 9.00 1.50 64.62 Spent FCC (75 wt. %) + 670 8.87 1.50 75.50 ZSM-5zeolite catalyst (25 wt. %) Spent FCC (62.5 670 8.95 1.50 74.71 wt. %) +ZSM-5 zeolite catalyst (37.5 wt. %) 100 wt. % ZSM-5 zeolite 670 8.971.50 77.89 catalyst

Example 11

Tests to determine the effect of starting temperatures on the aromaticscontent in liquid products boiling at a temperature below 240° C. wereconducted. The catalyst composition was 62.5 wt. % FCC catalyst and 37.5wt. % ZSM-5 zeolite catalyst, using a C/F feed ratio of 6. The resultsare presented in FIG. 10 and Table 14. As can be seen in FIG. 10, highercontent of aromatics in liquid product is obtained at temperatures of635 deg C. or higher.

TABLE 14 Dry catalyst Feed weight Aromatics Temperature, ° C. fedtransferred content 700 8.95 1.50 75.37 670 8.95 1.50 74.71 635 8.951.50 75.03 600 8.95 1.50 69.23

Example 12

Testing was conducted to determine the coke yields based on catalystcomposition. The catalyst composition used was spent FCC catalyst withvarying amounts of ZSM-5 zeolite catalyst of from 0 wt. % to 100 wt. %.A C/F ratio of 9 was used and the reactor temperature was 670° C. Theresults are presented in FIG. 11 and Table 15.

TABLE 15 ZSM-5 zeolite catalyst content Wt. % 0 25 37.5 50 100 in thecatalyst mixture C/F ratio g/g 9.07 9.0 9.0 9.0 8.92 Reactiontemperature at start ° C. 670 670 670 670 670 Dry catalyst fed g 6.806.77 6.76 6.75 6.70 Feed weight transferred g 0.75 0.75 0.75 0.75 0.75Coke yield Wt. % 5.72 4.86 4.93 4.59 4.58

Example 13

Test to determine the effect of reactor temperature at the start of thereaction on coke yields were conducted. The catalyst used was 62.5 wt. %FCC catalyst and 37.5 wt. % ZSM-5 zeolite catalyst used at a C/F feedratio of 9. The results are presented in FIG. 12 and Table 16.

TABLE 16 Catalyst Spent FCC Spent FCC Spent FCC Spent FCC composition,(62.5%) + (62.5%) + (62.5%) + (62.5%) + Wt. % ZSM-5 ZSM-5 ZSM-5 ZSM-5zeolite zeolite zeolite zeolite catalyst catalyst catalyst catalyst(37.5%) (37.5%) (37.5%) (37.5%) Reaction set 700 670 635 600 temperatureDry catalyst 6.75 6.76 6.77 6.80 fed Feed weight 0.75 0.75 0.75 0.75transferred Coke yield, 4.40 5.00 4.60 6.00 Wt. %From FIGS. 11 and 12 of Examples 12 and 13, respectively, it can be seenthat the coke yield varies in the region of 4 wt. % to 6 wt. %. In alarge scale conversion process like a FCC unit, the heat requirement forthe conversion process is met by heat generated by the combustion ofcoke made by the process and the unit is heat balanced. The amount ofcoke formation in the pyrolysis conversion process according to theinvention is adequate to support the required heat to balance a largescale continuous circulating fluidized bed riser—regenerator operationsand hence the coke made in the process is gainfully utilized to supportthe heat balance. Any deficiency in heat balance can be overcome byinjecting heavies (undesired product) or cracked product in the riser(additional olefins and coke make) or firing of heavy products inregenerator (fuel) without utilizing any other auxiliary fuel.

Example 14

Tests were conducted to determine the effect of adding feed separatelyfrom the catalyst mixture into the reactor and compared with the casewhen well mixed feed and catalyst were added together. In the case ofseparate addition of feed and catalyst, 6 gm of catalyst mixturecontaining 75 wt. % spent FCC catalyst and 25 wt. % ZSM-5 zeolitecatalyst was charged to the reactor and the reactor temperature wasallowed to stabilize. At a reaction temperature of 620° C., 1 g of theplastic feed mixture with the composition of Table 3 was charged to thereactor and the products were collected. In the second experiment, thesame quantities as above of a well mixed feed and catalyst were chargedinto a reactor where the start of reaction temperature was 620° C. Theproducts were collected. In both the studies the fluidization N₂ gasflow at 150 Ncc/min was employed. The results of these two studies arepresented in Table 17 below.

TABLE 17 Catalyst and feed Catalyst and feed Product yields chargedseparately charged together % Gas yield 45.7 47.9 % Liquid yield 50.448.0 % Coke yield 4.0 4.1 C4=, wt % 13.2 12.8 C3=, wt % 14.5 16.0 C2=,wt % 5.0 5.6 Total olefins 32.7 34.4

Slightly higher conversions were achieved when the feed and catalystwere mixed well and charged, although the conversions are similar. FromTable 17, it is clear that for effective utilization of catalyst, it ispreferable that the feed and catalyst mixing is uniform. Deeper catalystbeds may therefore not offer sufficient mixing with feed. Hence, goodmixing of feed and catalyst, preferably a co-current mixing of feed andcatalyst may help in better conversion of feed.

While the invention has been shown in only some of its forms, it shouldbe apparent to those skilled in the art that it is not so limited, butis susceptible to various changes and modifications without departingfrom the scope of the invention. Accordingly, it is appropriate that theappended claims be construed broadly and in a manner consistent with thescope of the invention.

We claim:
 1. A method of producing olefins and aromatic compounds from afeedstock, the method comprising: contacting a plastic feedstock and acatalyst composition at a temperature of 550° C. or higher, the catalystcomposition comprising a fluidized catalytic cracking (FCC) catalyst anda ZSM-5 zeolite catalyst, wherein the amount of ZSM-5 zeolite catalystmakes up at least 10 wt. % of the total weight of the FCC catalyst andthe ZSM-5 zeolite catalyst, the feedstock and the catalyst compositionbeing at a catalyst-to-feed ratio of from 6 or greater; and allowing atleast a portion of the feedstock to be converted to at least one ofolefins and aromatic compounds.
 2. The method of claim 1, wherein: theFCC catalyst is comprised of at least one of an X-zeolite, a Y-zeolite,a USY-zeolite, mordenite, faujasite, nano-crystalline zeolites, MCMmesoporous materials, SBA-15, a silico-alumino phosphate, agallophosphate, and a titanophosphate.
 3. The method of claim 1,wherein: the FCC catalyst is comprised of at least one of a Y-zeoliteand a USY-zeolite embedded in a matrix, the FCC catalyst having a totalsurface area of from 100 m²/g to 400 m²/g, coke deposition in an amountof from 0 to 0.5% by weight.
 4. The method of claim 1, wherein: the FCCcatalyst is a non-fresh FCC catalyst having from greater than 0 to 0.5%by weight of coke deposition.
 5. The method of claim 3, wherein: the FCCcatalyst has a total surface area of from 100 m²/g to 200 m²/g.
 6. Themethod of claim 1, wherein: the amount of ZSM-5 zeolite catalyst of thecatalyst composition makes up from 10 wt. % to 50 wt. % by total weightof the FCC catalyst and the ZSM-5 zeolite catalyst.
 7. The method ofclaim 1, wherein: the amount of ZSM-5 zeolite catalyst of the catalystcomposition makes up from 30 wt. % to 45 wt. % of the total weight ofthe FCC catalyst and the ZSM-5 zeolite catalyst.
 8. The method of claim1, wherein: the feedstock and the catalyst composition are contacted ata temperature of 570° C. to 730° C.
 9. The method of claim 1, wherein:the feedstock and the catalyst composition are at a catalyst-to-feedratio of from 8 or greater.
 10. The method of claim 1, wherein: theplastic feedstock comprises at least one of polyolefins, polyethylene,polypropylene, polystyrene, polyethylene terephthalate (PET), polyvinylchloride (PVC), polyamide, polycarbonate, polyurethane, polyester,natural and synthetic rubber, tires, filled polymers, composites,plastic alloys, and plastics dissolved in a solvent.
 11. The method ofclaim 1, wherein: the plastic feedstock and the catalyst composition arecontacted in a reactor that is at least one of a fluidized bed reactor,bubbling bed reactor, slurry reactor, rotating kiln reactor, and packedbed reactor.
 12. The method of claim 1, wherein: the FCC catalyst is anon-fresh FCC catalyst having from 0.2% to 0.5% by weight of cokedeposition.
 13. A method of producing olefins and aromatic compoundsfrom a feedstock, the method comprising: contacting a plastic feedstockand a catalyst composition at a temperature of 550° C. or higher, thecatalyst composition comprising a fluidized catalytic cracking (FCC)catalyst and a ZSM-5 zeolite catalyst, wherein the amount of ZSM-5zeolite catalyst makes up at least 10 wt. % of the total weight of theFCC catalyst and the ZSM-5 zeolite catalyst, the FCC catalyst being anon-fresh FCC catalyst having from greater than 0 to 0.5% by weight ofcoke deposition and having a total surface area of from 100 m²/g to 400m²/g, the feedstock and the catalyst composition being at acatalyst-to-feed ratio of from 6 or greater; and allowing at least aportion of the feedstock to be converted to at least one of olefins andaromatic compounds.
 14. The method of claim 13, wherein: the FCCcatalyst is comprised of at least one of an X-zeolite, a Y-zeolite, aUSY-zeolite, mordenite, faujasite, nano-crystalline zeolites, MCMmesoporous materials, SBA-15, a silico-alumino phosphate, agallophosphate, and a titanophosphate.
 15. The method of claim 13,wherein: the FCC catalyst is comprised of at least one of a Y-zeoliteand a USY-zeolite embedded in a matrix.
 16. The method of claim 13,wherein: the FCC catalyst is a non-fresh FCC catalyst having from 0.2%to 0.5% by weight of coke deposition.
 17. The method of claim 16,wherein: the FCC catalyst has a total surface area of from 100 m²/g to200 m²/g.
 18. The method of claim 13, wherein: the amount of ZSM-5zeolite catalyst of the catalyst composition makes up from 10 wt. % to50 wt. % by total weight of the FCC catalyst and the ZSM-5 zeolitecatalyst.
 19. The method of claim 13, wherein: the amount of ZSM-5zeolite catalyst of the catalyst composition makes up from 30 wt. % to45 wt. % of the total weight of the FCC catalyst and the ZSM-5 zeolitecatalyst.
 20. The method of claim 13, wherein: the feedstock is aplastic feedstock that comprises at least one of polyolefins,polyethylene, polypropylene, polystyrene, polyethylene terephthalate(PET), polyvinyl chloride (PVC), polyamide, polycarbonate, polyurethane,polyester, natural and synthetic rubber, tires, filled polymers,composites, plastic alloys, and plastics dissolved in a solvent.
 21. Amethod of producing olefins and aromatic compounds from a feedstock, themethod comprising: contacting a plastic feedstock and a catalystcomposition at a temperature of 550° C. or higher, the catalystcomposition comprising a fluidized catalytic cracking (FCC) catalyst anda ZSM-5 zeolite catalyst, wherein the amount of ZSM-5 zeolite catalystmakes from 10 wt. % to 50 wt. % of the total weight of the FCC catalystand the ZSM-5 zeolite catalyst, the FCC catalyst being a non-fresh FCCcatalyst having from 0.2% to 0.5% by weight of coke deposition andhaving a total surface area of from 100 m²/g to 200 m²/g, the feedstockand the catalyst composition being at a catalyst-to-feed ratio of from 6or greater; and allowing at least a portion of the feedstock to beconverted to at least one of olefins and aromatic compounds.